Oxidative desulfurization of sulfur-containing hydrocarbons

ABSTRACT

A method for desulfurizing a hydrocarbon stream ( 10 ) containing heterocyclic sulfur compounds, which process comprises contacting the heterocyclic sulfur compounds in the gas phase ( 60 ) in the presence of oxygen ( 70 ) with a supported metal oxide catalyst, or with a bulk metal oxide catalyst ( 600 ) to convert at least a portion of the heterocyclic sulfur compounds to oxygenated products as well as sulfur-deficient hydrocarbons and separately recovering the oxygenated products separately from a hydrocarbon stream with substantially reduced sulfur.

CROSS-REFERENCE TO RELATED APPLICATIONS

This application claims the benefit of U.S. Provision application Ser. No. 60/339,162.

This application is a National Stage application of co-pending PCT application PCT/US02/37600 filed Dec. 11, 2002, which was published in English under PCT Article 21(2) on Jun. 26, 2003; which claims the benefit of the U.S. Provisional application filed Dec. 13, 2001 cited below. These applications are incorporated herein by reference in their entireties.

BACKGROUND OF THE INVENTION

1. Field of the Invention

This invention broadly relates to a process for the removal and subsequent conversion of sulfur compounds found in hydrocarbons, especially refractory sulfur compounds found in petroleum streams (blend stocks) used to make gasoline and diesel fuel, to useful oxygenated hydrocarbon products and sulfur dioxide. Thus, the invention broadly relates to producing a hydrocarbon stream of a lowered sulfur content. The invention particularly relates to a catalytic gas phase oxidation process using a supported metal oxide catalyst or a bulk metal oxide catalyst for treating refractory sulfur compounds found in petroleum streams, such as used to make gasoline and diesel fuel, and converting them to useful oxygenated hydrocarbon products, such as maleic acid (anhydride), phenol, benzyl aldehyde and benzoic acid, and to sulfur dioxide. This method can also be extended to the removal of sulfur typically present in such sulfur containing hydrocarbons as gasoline and diesel fuels to yield sulfur dioxide and sulfur-deficient hydrocarbons.

2. Description of Related Art

Diverse types of petroleum feedstocks and streams contain sulfur compounds whose removal often is indispensable for commercial utilization of the feedstock or stream and/or for subsequent processing of the feedstock. In the face of ever-tightening sulfur specifications in transportation fuels, such as gasoline and diesel fuel, sulfur removal from petroleum feedstocks used to makes such fuels and from the petroleum fuel products themselves will become increasingly more important in years to come. In this regard, there have been several studies by the EPA concluding that the presence of sulfur in gasoline has an adverse impact on catalytic converters and, thus, tailpipe emissions from automobiles.

Sulfur deactivates conventional three-way Pt/Pd/Rh/Al₂O₃ catalytic converters designed to reduce hydrocarbon, CO and NOx emissions. Sulfur also degrades automobile diagnostic systems. Gasoline sulfur also prevents the introduction of more advanced catalytic technologies, such as Pt/BaO-based catalysts as NOx traps. For diesel fuels, the presence of sulfur produces an additional problem since particulate emissions created during combustion are increased in the presence of sulfur. There is special concern for particulates less than 2.5 microns since the EPA has concluded that there is a stronger link than ever between the tiniest soot particles and thousands of premature deaths each year. Consequently, both the EPA and the DOE have recommended that significantly limiting the level of sulfur in gasoline (15 ppm) and diesel fuels (30 ppm) would be essential for meeting lower vehicle emission standards in the future (by 2007). It is no surprise that substantial efforts have been expended to eliminate sulfur compounds from petroleum products.

Sulfur compounds routinely found in petroleum feedstocks and products include thiols (RSH), sulfides (RSR), disulfides (RSSR), saturated cyclic sulfides (C₂-C₅-cyclic sulfur-compounds, which incorporate sulfur into the saturated ring structure), thiophenes (primarily unsaturated C₄-cyclic sulfur compounds, where sulfur is incorporated into the unsaturated ring structure) and thiophene derivatives such as benzothiophene and dibenzothiophene (benzene rings that are fused to the sides of the thiophene (unsaturated C₄-cyclic sulfur compound) and various substituted benzothiophenes and dibenzothiophenes. Sulfur is the most abundant heteroatom impurity in petroleum crude and varies from 0.1 to 5 wt % depending on the geographic origin of the petroleum. After distillation of the crude oil, the sulfur content increases with the fraction's boiling point: naphtha (0.01-0.05% sulfur), kerosene (0.1-0.3% sulfur), gas oil (0.5-1.5% sulfur), atmospheric residue (2.5-5% sulfur), vacuum gas oil (1.5-3% sulfur), and vacuum residue (3-6% sulfur).

For the low boiling naphtha fraction, sulfur is mainly present as thiols, sulfides, disulfides or thiophene. For the middle boiling kerosene and gas oil fractions and especially the higher boiling fractions, thiophenic compounds, particularly benzothiophenes, dominate.

As a general rule, simple aliphatic, naphthenic, and aromatic mercaptans, sulfides, di- and polysulfides and the like surrender their sulfur more readily than the class of heterocyclic sulfur compounds comprised of thiophene and its higher homologs and analogs. Within the generic thiophenic class, desulfurization reactivity decreases with increasing molecular structure and complexity. While simple thiophenes represent the more labile sulfur types, the other extreme, sometimes referred to as “hard sulfur” or “refractory sulfur,” is represented by the derivatives of benzothiophene and dibenzothiophene, especially those mono- and di-substituted and condensed ring dibenzothiophenes bearing substituents on the carbons beta to the sulfur atom. These highly refractory sulfur heterocycles resist desulfurization.

Conventional technology removes sulfur from petroleum feedstocks via catalytic hydrodesulfurization (HDS). Hydrodesulfurization is one of the fundamental processes of the refining and petrochemical industries. In HDS, sulfur removal is typically achieved by reaction of the sulfur compounds with hydrogen over non-noble metal sulfides, especially those of Co/Mo/Al₂O₃ and Ni/Mo/Al₂O₃ catalysts, operating at elevated temperatures (˜400° C.) and extremely high pressures (˜100 atmospheres). Under these somewhat severe reaction conditions, (1) RSH, RSR and RSSR react to form hydrocarbons (RH), (2) saturated cyclic sulfides are converted to alkanes, (3) thiophene reacts largely to mixed isomers of butene (C₄H₈), (4) benzothiophene and its derivatives are initially hydrogenated to thiophane derivatives before removal of the sulfur atom to finally yield ethylbenzene (Bz-CH₂CH₃) and (5) dibenzothiophene is mainly converted to biphenyl with small amounts of phenylcyclohexene. The sulfur itself, along with the H₂, is ultimately converted to hydrogen sulfide. This H₂S is subsequently reacted with O₂ in the Claus process to H₂O and elemental sulfur, which is disposed in special landfills. An overall hydrogen balance for the HDS process reveals that the very valuable and expensive H₂ ultimately gets converted to invaluable H₂O.

Hydrogen consumption, thus, is an important consideration in these hydrodesulfurization (HDS) reactions because many of the components present in the feedstocks are more valuable as unsaturates, especially aromatics and olefins, and the hydrogenolysis of such components results in the production of light gases with marginal fuel values. In addition, during the manufacture of H₂ a significant amount of global warming CO₂ is generated during the very energy intensive steam reforming of methane, or steam reforming of lower hydrocarbons. The H₂ is typically generated by steam reforming of CH₄, or lower hydrocarbons, and the water-gas shift reaction as follows: CH₄+H₂O⇄CO+3H₂ CO+H₂O⇄CO₂+H₂.

Thus, the current HDS process technology converts valuable H₂ to invaluable H₂O, reduces the octane of the gasoline feedstocks, generates global warming CO₂ and elemental sulfur that needs to be disposed and is extremely energy intensive.

Notwithstanding these drawbacks, the petroleum industry has stated that HDS will be the preferred approach they will use to reduce sulfur levels in response to tighter regulatory controls because, HDS is a well-established and proven technology.

While HDS, as currently practiced, is known to provide nearly complete removal of mercaptans, sulfides and disulfides from liquid hydrocarbons, use of the current designs for reducing the level of thiophenes and other refractory sulfur compounds to a level of 30 ppm or below is problematic. In order to meet this very low level of sulfur, petroleum refiners will have to build additional capacity for generating additional hydrogen and will have to increase the reactor capacities of their HDS units or develop significantly more active HDS catalysts. Furthermore, efforts to drive the current HDS processes to increased sulfur removal is likely to lead to increased hydrogenation of the valuable fuel components and degradation in the fuel value (octane reduction) of the treated petroleum feedstock.

While HDS remains the predominant commercial approach for desulfurizing petroleum products, particularly petroleum feedstocks for making gasoline, the prior art has continued to develop and examine alternative processes. For example, various oxidative processes are known for removal of mercaptans by converting them to disulfides; such as the Merox™ process (see Handbook of Petroleum Refining Processes, R. A. Meyers, editor-in-chief, chapter 9.1, McGraw-Hill Book Company (1986)). It is also known to remove mercaptans and disulfides from petroleum feedstocks by adsorption with clays. U.S. Pat. No. 5,360,536 uses an adsorbent of a solid solution of metal oxides.

U.S. Pat. No. 5,935,422 describes a process for removal of organic sulfur compounds, particularly heterocyclic sulfur compounds, from petroleum feedstocks, and especially FCC feedstocks, by adsorption using zeolite Y exchanged with an alkali or alkaline earth metal cation and preferably impregnated with a group VIII metal. Regeneration of the sorbent is achieved by beating the sulfur-laden adsorbent in a hydrogen atmosphere.

The prior art also is exploring the use of biological removal processes (biodesulfurization). For example, U.S. Pat. No. 6,130,081 relates to a method of degrading organic sulfur compounds such as benzothiophene, dibenzothiophene and the like, by use of microorganisms belonging to the genus Paenibacillus and having the ability to decompose organic sulfur compounds, especially heterocyclic sulfur compounds, by specifically cleaving their C—S bonds under elevated temperature conditions.

Te et al., “Oxidative reactivities of dibenzothiophenes in polyoxometalate/H₂O₂ and formic acid/H₂O₂ systems,” Applied Catalysts A: General, 219(2001) 267-280 describes a liquid phase oxidation process potentially useful for removing refractory sulfur compounds from liquid hydrocarbon feed steams. The sulfur compounds are oxidized to sulfones and sulfoxides, which then can be extracted from the hydrocarbon. Other liquid phase oxidative approaches are described in EP 565 324 and U.S. Pat. No. 5,910,440 (biocatalytic).

I. G. Fedorchenko, N. N. Nechiporenko, V. I. Mitryaeva and E. N. Dubranovskaya, “Catalytic Activity of Certain Metal Oxides in Oxidation of Sulfur Compounds,” Vesten. Khar'kov. Politekh. Inst. 13 (1966):44-47 describes work involving the oxidation of thiophene over active metal oxides mixed with pumice, 1/4 ratio. Best results were obtained with Fe₂O₃, MoO₃ and Al₂O₃, but the reaction products obtained under the chosen reaction conditions were CO_(x), SO₂ and H₂O. A similar combustion study of thiophene was reported by V. A. Sslavinskaaya, D. Kreile, D. Eglite and I. Geimane, “Formation of Carbon Monoxide and Carbon Dioxide in the Vapor-Phase Oxidation of Heterocyclic Compounds on Vanadium-Molybdenum-Phosphorous Catalysts,” Latv. PSR Zinat. Akad. Vestis, Kim. Ser. 6 (1971): 735-738. These investigators employed a V—Mo—P catalyst.

Another interesting investigation of thiophene oxidation over a 10% MoO₃ and TiO₂ mixed metal oxide catalyst is reported by M. Blanchard and J. Goichon, “Heterogeneous Catalytic Oxidation of Aromatic Sulfur Compounds: Thiophene and Benzothiophene,” Bull. Soc. Chim. Fr. 1-2/Pt. 2 (1975): 289-290. The oxidation yielded 75% selectivity towards maleic anhydride and thiomaleic anhydride at moderate conversions. Supported MoO₃/TiO₂ and bulk V₂O₅ were also found to be efficient catalysts for the selective oxidation of thiophene to maleic products. In addition, oxidation of benzothiophene over the 10% MoO₃—TiO₂ catalyst quantitatively yielded phenol with 100% selectivity.

U.S. Pat. No. 5,969,191 describes a catalytic thermochemical process, which can be used for converting by-products from pulp and paper mills (TRS compounds including mercaptans) to a valuable chemical intermediate (H₂CO), which is consumed in the pulp and paper Industry. A key catalytic reaction step in the thermochemical process scheme is the selective catalytic oxidation of organosulfur compounds (e.g., CH₃SH+2O₂→H₂CO+SO₂+H₂O) over certain supported (mono-layered) metal oxide catalysts. The preferred commercial catalyst employed in this process consists of a specially engineered V₂O₅/TiO₂ catalyst that minimizes the adverse effects of heat and mass transfer limitations that can result in the over oxidation of the desired H₂CO to COx and H₂O.

BRIEF DESCRIPTION OF THE DRAWINGS

FIG. 1 is a schematic drawing of a process of the present invention.

FIG. 2 is another schematic drawing of a process of the present invention.

FIG. 3 is still another schematic drawing of a particularly preferred process of the present invention.

FIG. 4 illustrates the results of Temperature Programmed Surface Reaction-Mass Spectrometry experiments.

FIG. 5 illustrates another result of the Temperature Programmed Surface Reaction-Mass Spectrometry experiment.

BRIEF DESCRIPTION OF THE INVENTION

The present invention is directed to a process for removing sulfur compounds found in a hydrocarbon stream, e.g., in a petroleum feedstock or petroleum product, and converting such sulfur compounds, or sulfinyl (═SO) or sulfonyl (═SO₂) derivatives thereof, to sulfur dioxide and to useful oxygenated products as well as sulfur-deficient hydrocarbons by vapor phase oxidative desulfurization of the sulfur compounds, or the sulfinyl (═SO) or sulfonyl (═SO₂) derivatives thereof, removed from such hydrocarbon stream. The sulfur compounds, or sulfinyl (═SO) or sulfonyl (═SO₂) derivatives thereof in the gas phase are contacted with a supported metal oxide catalyst, or with a bulk metal oxide catalyst in the presence of oxygen for a time sufficient to convert at least a portion of the heterocyclic sulfur compounds, or the sulfinyl (═SO) or sulfonyl (═SO₂) derivatives thereof, to oxygenated products and sulfur-deficient hydrocarbons and recovering a hydrocarbon stream with substantially reduced sulfur separately from the oxygenated products. The process not only results in the removal of sulfur compounds from such petroleum feedstocks, such as gasoline and diesel feedstocks, but actually provides for the efficient upgrading of various cyclic sulfur compounds found in these petroleum feedstocks (e.g., C₂-C₅ saturated cyclic-sulfur compounds, thiophenes, benzothiophenes and dibenzothiophenes) to valuable chemical products (C₂-C₅ hydrocarbons and/or oxygenated hydrocarbons, maleic anhydride, phenol, benzoic acid and H₂SO₄ or elemental sulfur). The oxidative desulfurization process thus reduces the sulfur content of hydrocarbon streams without the need for additional hydrogen consumption.

According to the present invention, the sulfur compound impurities found in a gaseous hydrocarbon feed stream containing such sulfur impurities, especially refractory sulfur compounds such as thiophenes, benzothiophenes, and dibenzothiophenes and their higher boiling derivatives, or the sulfinyl (═SO) or sulfonyl (═SO₂) derivatives thereof, are contacted in the presence of oxygen with a supported metal oxide catalyst. A supported metal oxide catalyst comprises a metal oxide support having supported thereon a layer, preferably only a monolayer, of a catalytic metal oxide. The catalytic metal oxide layer supported by the metal oxide support used in the process of the present invention is typically based on a metal selected from the group consisting of titanium (Ti), zirconium (Zr), molybdenum (Mo), rhenium (Re), vanadium (V), chromium (Cr), tungsten (W), manganese (Mn), niobium (Nb), tantalum (Ta) and mixtures thereof. The metal oxide support for the supported metal oxide catalyst generally is selected from titania (TiO₂), silica (SiO₂), zirconia (ZrO₂), alumina (Al₂O₃), ceria (CeO₂), magnesia (MgO), niobia (Nb₂O₅), tantala (Ta₂O₅), manganates (MnO_(x)), lanthanum oxide (La₂O₃), tin oxide (SnO₂) and mixtures thereof. Generally, a support of titania, zirconia, ceria, niobia, tin oxide or their mixture is preferred.

As a general rule, titanium (Ti), zirconium (Zr), niobium (Nb), tantalum (Ta) and tungsten (W) should not be used as the sole catalytic species with a silica support, nor should the metal oxide support and the supported metal oxide of the catalyst be the same.

In a generally less preferred alternative embodiment of the present invention, the process also can be carried out using a bulk metal oxide catalyst wherein the bulk metal oxide, and especially the bulk mixed metal oxide, is based on molybdates (Mo), chromates (Cr), vanadates (V), rhenates (Re), titanates (Ti), niobates (Nb), tantalates (Ta), tungstates (W), manganates (Mn) and mixtures thereof. Bulk metal oxide catalysts based on molybdenum, chromium and vanadium are preferred.

The preferred supported metal oxide catalyst compositions (mono-layered catalysts) and the bulk metal oxide catalyst compositions, useful for practicing the present invention, are known in the prior art, as are their methods of production.

DETAILED DESCRIPTION OF THE INVENTION

Hydrocarbon feedstocks suitable for treatment using the present invention are those petroleum-based feedstocks, which contain condensed ring sulfur heterocyclic compounds. Such compounds are typically found in petroleum streams boiling in the distillate range and higher. Non-limiting examples of such feedstocks include a catalytically cracked gasoline stream (e.g., cracked naphtha), generally from a fluid catalytic cracker (FCC gasoline) or thermal catalytic cracker (TCC), a heavy straight run gasoline stream, generally obtained by atmospheric distillation of a crude, an aromatic saturated gasoline stream, diesel fuels and jet fuels. Such feeds typically have a boiling range from about 150 to about 600° C., usually from about 175 to about 400° C. In the broad practice of this invention, any hydrocarbon stream containing refractory sulfur compounds can be treated, since their boiling point temperatures at atmospheric pressure are: thiophene (84° C.), 2,5-dimethylthiophene (134° C.), 1-benzothiophene (222° C.), dibenzothiophene (333° C.), 4-methyldibenzothiophene (298° C.) and 4,6-dimethyldibenzothiophene (estimated to be ˜250-380° C.).

There is a well-established hierarchy in the ease of sulfur removal from the various organo-sulfur compounds common to petroleum streams. Simple aliphatic mercaptans, naphthenic mercaptans, and aromatic mercaptans, sulfides, di-sulfides and polysulfides and the like generally surrender their sulfur content more readily than the class of heterocyclic sulfur compounds comprised of thiophene and its higher homologs and analogs. Within the generic thiophenic class, desulfurization reactivity also decreases with increasing molecular structure and complexity. While simple thiophenes represent the more labile sulfur types in this class, the other extreme, which is sometimes referred to as “hard sulfur” or “refractory sulfur,” is represented by the derivatives of benzothiophene and dibenzothiophene, especially those mono-substituted and di-substituted and condensed ring dibenzothiophenes. An example of a typical three-ring “hard” sulfur compound found in petroleum streams is 4,6-dimethyldibenzothiophene, or 4,6-DMDBT for short. These highly refractory sulfur heterocycles resist desulfurization as a consequence of steric inhibition. For this reason, these materials often survive traditional desulfurization processes, e.g. hydrodesulfurization, and remain in the hydrocarbon stream as a potential poison for subsequent processes whose operability is dependent upon a sulfur sensitive catalyst. Destruction of these “hard sulfur” types can be accomplished under relatively severe process conditions in HDS, but this is undesirable owing to the onset of harmful side reactions leading to feed and/or product degradation and excessive hydrogen consumption.

While the desulfurization process of the present invention is potentially applicable to all sulfur bearing compounds common to petroleum streams, it is particularly suitable for the oxidative desulfurization of the least reactive, more highly refractory sulfur species, such as those derived from thiophenes, benzothiophenes and dibenzothiophenes. As used throughout the specification and claims, therefore, the term “refractory sulfur” and similar terms is intended to embrace thiophene, benzothiophene, dibenzothiophene, and the higher boiling derivatives of these sulfur compounds. In addition, to these sulfur compounds, the present invention also embraces the sulfinyl (═SO) or sulfonyl (═SO₂) derivatives of thiophene, benzothiophene, dibenzothiophene, and their higher boiling derivatives.

The process of the present invention generally will result in a hydrocarbon stream with substantially reduced sulfur, a sulfur dioxide stream and separate streams of oxygenated hydrocarbon products. For purposes of this invention, the term, “substantially reduced sulfur”, depends upon the overall process being considered, but can be defined as a sulfur content less than about 100 wppm, preferably less than about 50 wppm, more preferably less than about 30 wppm, and most preferably less than about 10 wppm as measured by existing, conventional analytical technology.

In accordance with the present invention, and with reference to FIG. 1, a sulfur-containing hydrocarbon gas stream 10, preferably containing and enriched amount of refractory sulfur compounds such as thiophene, benzothiophene, dibenzothiophene and their higher boiling derivatives, is introduced into a reactor 60. The level of such sulfur compounds can be enriched in such steam using known techniques of absorption, adsorption, extraction and the like. Air or an oxygen-enriched gas generally is added via stream 20 to establish oxidizing conditions in reactor 60. Reactor 60 contains a supported metal oxide catalyst (preferably mono-layered), or a bulk metal oxide catalyst, in a form suitable for conducting the oxidation reactions. The selective oxidation that occurs in reactor 60 produces a gas stream containing the oxygenated hydrocarbon products, sulfur dioxide, H₂O, CO_(x) and unreacted hydrocarbons and sulfur compounds, which exits reactor 60 in gas stream 30. The oxygenated products may include maleic anhydride, phenol, benzyl aldehyde, benzoic acid and the like depending upon the nature of the sulfur compounds in gas stream 10.

As noted, the oxidizing agent used in the selective oxidation can usually be oxygen or air. The contacting of the, sulfur-containing hydrocarbon gas stream with the supported metal oxide catalyst or bulk metal oxide catalyst under an oxidizing atmosphere, e.g., in the presence of oxygen, and at an appropriate temperature, causes a selective oxidation of the sulfur compounds to the valuable oxygenated products and sulfur deficient hydrocarbons.

The optimum reaction time in reaction zone 60 (space velocity) varies with temperature, pressure and the molar ratio of the reactants. The space velocity likely will be maintained below about 4800 V/V/hr. As a general rule, higher conversions are associated with lower space velocities, e.g., a space velocity of 5 to 200 volume of gas (STP) per volume of catalyst per hour. In the broad practice of the invention, space velocities of up to 2000 volumes of gas (STP) per volume of catalyst per hour are generally contemplated.

A variety of oxygenated species, such as maleic anhydride, phenol, benzyl aldehyde and benzoic acid, are the intended products of the present process and can be recovered from the gaseous reaction product via stream 40, separate from byproduct SO₂ and the CO_(x) via stream 80 and separate from unreacted (sulfur depleted) hydrocarbons and unconverted sulfur-containing compounds via stream 70, using any one of a number of separation options (zone 50) known to those skilled in the art.

The selectivity of the oxidation of the organosulfur compounds to the valuable oxygenated products and the sulfur-deficient hydrocarbons has its origin in the preferential attack of oxygen at the C—S bonds of the organosulfur compounds, in the vicinity of the catalytic surface sites, because of the weak C—S bonds relative to strong C—O bonds. The nature of the products resulting from the gas phase oxidation suggests that the initial oxygen atoms are attached to the carbon atoms adjacent to the sulfur atom and that the thiomaleic anhydride can be completely converted to maleic anhydride at conversions approaching 100%. Over-oxidation of maleic anhydride to COx and H₂O should not be a significant problem since anhydrides are known to be relatively stable (especially compared to the reactive C—S—C bond in thiomaleic anhydride).

Maleic anhydride, expected to be produced by the selective oxidation of thiophene and some of the higher refractory sulfur compounds, is an important chemical intermediate that is currently produced by selective oxidation of n-butane over bulk VPO catalysts, with annual production ˜2 billion pounds. Phenol, another of the expected products from the selective oxidation of benzothiophene, ranks third among the secondary products of benzene, one of the world's ten top bulk organic chemicals, and annual synthetic phenol production is ˜5 billion pounds. The current technology to synthesize phenol from benzene is very complicated and consumes much energy and produces significant waste by-products. For example, phenol production via the classical benzenesulfonic acid process yields 1.35 pounds of Na₂SO₃ and 2.1 pounds Na₂SO₄ as by-products for every pound of phenol. Moreover, a three-stage distillation is required for phenol purification. The present process, thus provides a useful alternative source of this valuable chemical. Benzyl aldehyde, benzoic acid and maleic anhydride may also form from benzothiophene.

Saturated cyclic sulfides are expected to be converted to dialdehydes and glycols (via hydrogenation), which also are valuable chemical intermediates. Of special interest is the saturated C₂ cyclic sulfide, which should be oxidized to C₂-dialdehyde and can be hydrogenated to ethylene glycol, ˜7 billion pounds annual production. The saturated C₅ cyclic sulfide also is expected to be oxidized to maleic anhydride since n-pentane is oxidized to maleic anhydride.

As will be recognized by those skilled in the art, the gas stream 30 leaving the reactor will contain the hydrocarbon feedstock and may contain unreacted sulfur compounds, as well as the oxygenated products, sulfur dioxide, carbon oxides and water. Principal by-products of the oxidative desulfurization that may be formed are carbon monoxide, which may be accompanied by carbon dioxide (possibly in a minor amount) and sulfur dioxide. COS may also be a minor product.

The reaction mixture leaving the reactor 60 in gas stream 30 is generally subject to further processing in zone 50 in a conventional manner. For example, a concentrated stream of the oxygenated products 40 can be recovered in a washer, or by indirect cooling, or also by fractional cooling. For example, the washing can be performed with an aqueous stream, in which case a multi-stage washer can be used. An aqueous stream 40 containing the oxygenated products can be obtained in this manner separate from the sulfur dioxide and carbon oxides in stream 80. An advantage of the vapor-phase route is the ease with which SO₂ and CO_(x) can be separated from the reaction products because of their very high vapor pressure and any residual SO₂ can be readily removed with an ion exchange column. With judicious selection of metal oxide catalyst, the sulfur-containing compounds that are typically present in petroleum feedstocks and other petroleum products are expected to be selectively oxidized to valuable chemical intermediates or sulfur-deficient hydrocarbons.

The sulfur dioxide can be disposed of by any technique known in the art. For example, the sulfur oxide (from stream 80) can be oxidized and converted to sulfuric acid. The sulfuric acid can then be used directly in the petroleum refinery for purposes well known to those skilled in the art. The crude stream 40 of the oxygenated products then can be treated, such as by distillation, for recovering a purified stream of, for example, maleic anhydride and other oxygenated species. Fractional condensation also can be used to obtain a desired oxygenated product. Other ways for individually isolating the oxygenated products will be apparent to those skilled in this art. The residual gas 80, likely containing carbon monoxide as well, may be treated (so as to recover sulfur oxides). The remaining fraction in stream 70 containing the original hydrocarbon fraction and any unreacted sulfur compounds can be recycled to the oxidative desulfurization reactor 60 (not shown) following any heating that may be needed to convert the stream into a gas, or may be sufficiently low in sulfur to be returned to the refinery for use as a gasoline feed stock.

For obtaining higher yields and selectivities, the conditions of the oxidative desulfurization can be varied. For example, the pressure, temperature, composition of the starting gas mixture, the amount of catalyst and/or the rate of flow can be varied. The reactor effluent remaining after separation of the oxygenated products and by-products can then be recycled (not shown) into the reactor 60.

A key feature of the present invention is the use of a heterogeneous gas phase reaction conducted in the presence of certain metal oxide supported catalysts (preferably mono-layered catalysts), or bulk metal oxide catalysts, between the sulfur compounds and oxygen. The metal oxide of the supported metal oxide catalyst is accommodated in the support primarily as a two-dimensional metal oxide overlayer (preferably a mono-layer), with the oxide having a non-crystalline form. Supported metal oxide catalysts useful in the process of this invention generally comprise a metal oxide substrate, or support, such as titania, silica, zirconia, alumina, niobia, tantala, ceria, magnesia, manganates, lanthanum oxide, tin oxide and mixtures thereof, whose surface has been modified with a layer (preferably no more than a monolayer) of an oxide of a catalytic metal or a mixture of catalytic metal oxides as identified above (e.g., preferably an oxide of vanadium, and oxide mixtures containing vanadium) in an amount such that the catalyst exhibits properties different from the metal oxide substrate whose surface has not been modified. The support and the supported metal should not be the same.

Consequently, in this preferred embodiment of the invention, the metal oxide loading (preferably vanadium oxide) on the metal oxide support or substrate, e.g., a titania support, must be sufficient to modify the metal oxide surface. The metal oxide loading on the metal oxide support or substrate broadly ranges between about 0.5 to 35 wt % of the total catalyst weight.

The preferred vanadia (vanadium oxide) on titania, supported metal oxide catalyst used in this process has at least a portion, preferably at least about 25 wt %, and most preferably substantially all of said supported vanadium oxide in a non-crystalline form.

A preferred metal oxide support for use in the process of this invention is titania (titanium dioxide), which can be employed in the anatase or rutile form. For example at least about 25 wt % (and generally from about 50 to about 100 wt %) of the titanium dioxide (TiO₂) can be in the anatase form. As recognized by those skilled in the catalytic art, the titania support material needs to be judiciously evaluated since certain grades may have impurities that interfere with the catalytic activity. Normally, with recognition of the previous caveat, the titanium dioxide may be prepared by any conventional technique. The titanium dioxide used in the catalyst of this invention may be composed of substantially porous particles of a diameter of from about 0.4 to about 0.7 micron and preferably has a specific surface area of at least about 1 m²/g, more usually at least about 5 m²/g, preferably at least about 40 m²/mg and sometimes at least about 100 m²/g.

The metal oxide supported catalysts used in the process of this invention may be prepared by impregnation techniques well-known in the art, such as incipient wetness, grafting, equilibrium adsorption, vapor deposition, thermal spreading, etc. When using an incipient wetness impregnation technique, an aqueous or non-aqueous solution containing a metal oxide precursor compound is contacted with the metal oxide support or substrate material, e.g., titania, for a time sufficient to deposit a metal oxide precursor material onto the support such as by selective adsorption or alternatively, excess solvent may be evaporated leaving behind the precursor compound or salt. If an incipient wetness impregnation technique is used to prepare a catalyst of this invention, the metal oxide precursor (e.g., salt) solution used may be aqueous or organic, the only requirement being that an adequate amount of a precursor compound for the selected metal oxide be soluble in the solvent used in preparing this solution. Other impregnation techniques, such as vapor deposition and thermal spreading, do not require use of a solvent as does incipient wetness, and may be desirable in some circumstances to avoid the problem of volatile organic carbon (VOC) emissions.

One way to disperse vanadium oxide, tungsten oxide or a combination of the two oxides onto a titania metal oxide support or substrate is to impregnate titania spheres or powder (spheres or powder are used as representative examples of shapes of titania) with a solution containing a vanadium or a tungsten compound. When impregnating a substrate with both oxides, the tungsten and vanadium are introduced in a stepwise manner, tungsten first, followed by vanadium, with appropriate intermediate drying and calcining steps. Each solution may be an aqueous solution, one using an organic solvent or a mixture of the two. Generally, an aqueous solution is preferred. Criteria used to choose the vanadium and tungsten compounds include whether the compounds are soluble in the desired solvent and whether the compounds decompose at an acceptable rate at a high, calcination temperature to give the appropriate metal oxide overlayer. Illustrative of suitable compounds of vanadium and tungsten are the halides of vanadium and tungsten, oxyacids, oxyacid salts and oxysalts of vanadium and tungsten. Specific examples or precursors are tungsten dibromide, tungsten pentabromide, tungsten tetrachloride, tungsten dioxydichloride, tungstic acid, ammonium meta-tungstate, vanadium tribromide, vanadium dichloride, vanadium trichloride, vanadium oxychloride, vanadium oxydichloride, vanadic acid, vanadyl sulfate, vanadium alkoxides, vanadium oxalate (which may be formed in situ by reaction of V₂O₅ and an aqueous solution of oxalic acid), and ammonium meta-vanadate. Suitable metal oxide precursor compounds for the other metal species suitable for making the supported metal oxide catalysts of this invention are well recognized by those skilled in the catalysis art.

The impregnation of the metal oxide support or substrate, e.g., titania support in the form of spheres or powder, with the metal oxide precursor compound solution may be carried out, as noted above, in ways well known in the art using either wet or dry impregnation techniques. One convenient method is to place the metal oxide support or substrate, e.g., titania particles, into a rotary evaporator, which is equipped with a steam jacket. An impregnating solution of a precursor compound which contains an amount of the desired metal to be included in the finished catalyst (as the metal oxide) is added to the support particles and the mixture is cold rolled (no steam) for a time from about 10 to 60 minutes sufficient to impregnate the support with the precursor compound solution. Next, steam is introduced and the solvent is evaporated from the impregnated solution. This usually takes from about 1 to about 4 hours. The impregnated support will normally be dried at temperatures ranging from about 50°-300° C. to remove excess solvent.

Water-soluble precursor compounds are generally preferred for industrial applications because of the environmental concern about VOC emissions. Nonetheless, when using an organic solvent, initial heating may be done in a nitrogen atmosphere to remove any flammable solvent. Finally, the support particles are removed from the rotary evaporator and calcined in a suitable oxidizing atmosphere such as air, oxygen, etc. at a temperature of about 150° to 800° C., and more usually from 400°-600° C., preferably for about 1 to about 3 hours, sufficient to decompose the precursor compound to the corresponding metal oxide. In other cases, as recognized by those skilled in the art, calcining conditions need to be adjusted to avoid undesirably reducing the surface area of the metal oxide support.

Because some precursor compounds are air/moisture sensitive, they are prepared under a nitrogen atmosphere as is recognized by those skilled in this art. The time required to calcine the composite will, of course, depend on the temperature and in general will range from about 0.5-7 hours. Calcination at 450° C. for about 2 hours has proven to be suitable for 1% vanadia on titania catalysts. The precise time and temperature for calcination depends on the particular metal oxide overlayer and should be selected, as well-recognized by those skilled in the art, to avoid adversely affecting the metal oxide support, e.g. in the case of a titania metal oxide support, to avoid substantial crystal phase transformation of the anatase into another crystalline form, e.g., rutile, and degradation of extended surface area.

Reducing atmospheres may also be used to decompose the transition metal oxide precursors. To avoid potential safety concerns, the resulting composite should be calcined to convert the reduced metal component to the oxide form. If the support is to be provided with an overlayer of a combination of metal oxides, e.g., if an overlayer containing both vanadium oxide and tungsten oxide is desired, then the metal oxide precursor compounds may be impregnated on the metal oxide support simultaneously, but preferably are impregnated sequentially. The metal oxide supported catalysts used in the process of this invention will generally have surface metal oxide loadings of from about 0.5 to 35 wt. % metal oxide based on the total active catalyst composition, preferably from about 1 to 20 wt. %, more usually from about 1-15 wt. %, and most preferably 1-10 wt. % based on the total active catalyst composition. The intent, generally, is to provide no more than a monolayer of the catalytic oxide overlayer on the metal oxide support.

Titania, silica, zirconia, alumina, niobia, tantala, ceria, magnesia, manganates, lanthanum oxide and tin oxide are conveniently referred to as supports or substrates in the description of the preferred embodiment of the present invention, based to a large degree on the way the catalyst is prepared. Nonetheless, it should be noted that these metal oxides also provide important roles as active catalytic components in the supported metal oxide catalyst. Combination supports may also be advantageous for use in catalysts suitable for practicing the process of this invention. For example, substrates constituting a mixture of titania and zirconia, or titania and silica can be used.

Further details on the preparation and structure of such metal oxide supported catalysts useful in the practice of the present invention can be found, inter alia, in Jehng et al., Applied Catalysis A, 83, (1992) 179-200; Kim and Wachs, Journal of Catalysis, 142, 166-171; Jehng and Wachs, Catalysis Today, 16, (1993) 417-426; Kim and Wachs, Journal of Catalysis, 141, (1993) 419-429; Deo et al., Applied Catalysis A, 91, (1992) 27-42; Deo and Wachs, Journal of Catalysis, 146, (1994) 323-334; Deo and Wachs, Journal of Catalysis, 146, (1994) 335-345; Jehng et al., J. Chem. Soc. Faraday Trans., 91(5), (1995) 953-961; Kim et al. Journal of Catalysis, 146, (1994) 268-277; Banares et al., Journal of Catalysis, 150, (1994) 407-420 and Jehng and Wachs, Catalyst Letters, 13, (1992) 9-20, the disclosures of which are incorporated herein by reference.

For the supported metal oxide catalyst, the preferred vanadium oxide may preferably be used in mixture with an oxide of one of molybdenum (Mo), tungsten (W), chromium (Cr), rhenium (Re), and manganese (Mn), supported on titania or silica. In the case of a vanadia on silica catalyst, an adjuvant selected from the group consisting of an oxide of titanium, zirconium, cerium, tin, niobium and tantalum, should generally be present to enhance catalytic activity. A particularly preferred supported metal oxide catalyst is one comprising a vanadia overlayer (monolayer) on a titania support.

It often is desired that the metal oxide support, such as titania, silica, zirconia, alumina, niobia, tantala, magnesia, ceria, manganates, lanthanum oxide, tin oxide, and their mixtures, used as a catalyst support component in accordance with the present invention have a surface area in the range of about 1 to about 150 m²/g and higher. These materials may be used in any configuration, shape or size, which exposes their surface and any metal oxide overlayer dispersed thereon, to the gaseous stream passed in contact therewith. For example, these oxide supports, such as titania can conveniently be employed in a particulate form or deposited (before or after impregnation with the metal oxide overlayer) on a monolithic carrier or onto ceramic rings or pellets. As particles, the support, such as titania, can be formed in the shape of pills, pellets, granules, rings, spheres and the like. Use of free particulates might be desirable when large catalyst volumes are needed or if the catalyst bed is operated in a fluidized state. A monolithic form, or deposition of the active catalyst on an inert ceramic support might be preferred in applications where catalyst movement is to be avoided because of concerns about catalyst attrition and dusting, and a possible increase in pressure drop across a particulate catalyst bed. In a preferred approach, a metal oxide supported catalyst, such as a vanadia on titania catalyst, may be deposited on a ceramic carrier such as silicon carbide, silicon nitride, carborundum steatite, alumina and the like, provided in the shape of rings or pellets. Typically, the active catalyst will be applied to the inert ceramic support in an amount to provide 1 to 15% by weight of the supported catalyst.

As noted, the present invention also contemplates the use of bulk metal oxides as the catalyst for converting petroleum sulfur compounds into oxygenated products. Such bulk metal oxide catalysts generally constitute molybdates (Mo), chromates (Cr), vanadates (V), rhenates (Re), titanates (Ti), niobates (Nb), tantalates (Ta), tungstates (W), manganates (Mn) and mixtures thereof. Such metal oxides also contain a wide variety of other metal species such as alkali metals (e.g., sodium (Na), lithium (Li), potassium (K) and cesium (Cs)), alkaline earth metals (e.g., calcium (Ca), barium (Ba), and magnesium (Mg)) and transition metals (e.g., copper (Cu), nickel (Ni), cobalt (Co), aluminum (Al), lead (Pb), bismuth (Bi), iron (Fe), zinc (Zn), cadmium (Cd), tellurium (Te), manganese (Mn)). Those skilled in the art recognize the wide variety of available bulk metal oxide catalysts.

Methods for making bulk metal oxide catalysts used in the present invention also are well known to those skilled in the art. In particular, the active catalyst can be prepared by physically blending the metal oxides, by coprecipitation from aqueous solutions containing soluble compounds of the catalyst components in the desired molar ratio or by any other technique, which provides an intimate mixture of the metal oxide constituents. For example, an aqueous solution of a water-soluble molybdenum compound (ammonium heptamolybdate) is mixed with a water-soluble iron compound (ferric chloride) to cause coprecipitation of both molybdenum and iron, using procedures well known to those skilled in the art. The coprecipitate is washed, to eliminate the soluble salts formed during the coprecipitation reactions, filtered, dried and calcined to convert the metal constituents to their active iron molybdate (oxide) form. Those skilled in the art recognize a variety of water-soluble metal compounds that can be used to prepare the active bulk metal catalyst. Alternatively, oxides of the respective metals may be ground together and calcined. Additional details on bulk metal oxides and bulk metal oxide catalysis can be found in Arora et al., Journals of Catalysis, 159, (1996) 1-13, which is incorporated herein by reference.

Those skilled in the art recognize that there exists a wide range of compounds, generally used in admixture, suitable for preparing bulk metal oxide catalysts. The following is a representative, though not exhaustive, list of possible constituents: bulk vanadates such as PbV₂O₆, NaVO₃, Na₃VO₄, BiVO₄ and other Bi—V—O family members, AlVO₄, FeVO₄, Mg₃(VO₄)₂, Mg₂V₂O₇, CeVO₄, Zn₃(VO₄)₂, CdV₂O₇, Zn₂V₂O₇, VOPO₄ and other V—P—O family members, KVO₃, Pb₂V₂O₇, and TIVO₄; bulk molybdates such as PbMoO₄, CaMoO₄, Bi₂Mo₂O₉, Bi₃(FeO₄)(MoO₄)₃ and other Bi—Mo—O family members, Na₂MoO₄, MnMoO₄, Gd₂(MoO₄)₃, MgMoO₄, CuMoO₄, CoMoO₄, Fe₂(MoO₄)₃, Te₂MoO₇, NiMoO₄, Al₂(MoO₄)₃, Cr₂(MoO₄)₃, and Na₂Mo₂O₇; bulk niobates such as YNbO₄, YbNbO₄, LiNbO₃, NaNbO₃, KNbO₃, AlNbO₄, K₈Nb₆O₁₉, BiNbO₄, and other Bi—Nb—O family members, SbNbO₄, NbOPO₄, CaNb₂O₆, K₄Nb₆O₁₇, and KCa₂Nb₃O₁₀; bulk tungstates such as Li₆WO₆, FeWO₄, CoWO₄, MnWO₄, NiWO₄, CuWO₄, CaWO₄, Cs₂WO₄, Na₂WO₄, B_(a)WO₄, Fe₂(WO₄)₃, Al₂(WO₄)₃, SrWO₄, K₂WO₄, Na₂W₂O₇, Li₂WO₄, CsLuW₂O₈, BiWO₄, and other Bi—W—O family members; bulk chromates such as Na₂CrO₄, Na₂Cr₂O₇, Na₂Cr₃O₁₀, Na₂Cr₄O₁₃, K₂CrO₄, K₂Cr₂O₇, K₂Cr₃O₁₀, K₂Cr₄O₁₃, Fe₂(CrO₄)₃, CaCrO₄, Cs₂CrO₄; BiCrO₄ and other Bi—Cr—O family members; bulk rhenates such as NaReO₄, Li₆ReO₄, and Mg(ReO₄)₂; bulk titanates such as Na₂TiO₄, NaTiO₃, BaTiO₄, BaTiO₃, and other Ba—Ti—O as well as Bi—Ti—O family members and bulk manganates such as Mn₃(VO₄)₂, MnAl₂O₄, KMnO₄, MnO, MnO₂, Mn₂O₃, and Mn₃O₄.

To achieve high selectivity in the conversion of the petroleum sulfur compounds to the oxygenated compounds, it is important to maintain the flow rate of reactant gas per unit mass of catalyst in the range of 10⁻² to 10⁴ cubic centimeters (STP) of reactants per gram of active catalyst per minute (excluding inert ceramic components or other inert support material). Generally, higher reaction temperatures permit higher flow rates. Usually, the process can be operated at 10⁻¹ to 10², cubic centimeters (STP) of reactants per gram of catalyst per minute.

The oxidation reaction involving the noted refractory sulfur compounds is exothermic. As recognized by those skilled in the art a variety of reactor designs may be employed, such as a tubular reactor, to accommodate the necessary mass and heat transfer processes for effective operation on a continuous basis, semi-continuous or batch basis. Packed catalyst beds and fluid bed operation are contemplated as possible embodiments. The oxidation reaction may be conducted at atmosphere pressure, and above or below atmospheric pressure.

Among the aromatic heterocyclic sulfur compounds of particular interest in this application are thiophene, 2-methylthiophene, 3-methylthiophene, 2-ethylthiophene, benzothiophene, and dimethylbenzothiophene, as well as higher boiling derivatives. Mercaptans which can also be removed by the process of this invention often contain from 3-10 carbon atoms, and are illustrated by materials such as 1-mercaptopropane, 2-mercaptopropane, 1-mercaptobutane, 2-mercaptobutane, 2-methyl-2-mercaptopropane, mercaptopentanes, mercaptohexanes, mercaptoheptanes, mercaptooctanes, mercaptononanes, and mercaptodecanes. The total sulfur content in hydrocarbon feedstocks usually is in the range from about 150 ppm to as much as several thousand ppm and higher. Indeed, hydrocarbon streams containing as much as 5% sulfur are often encountered. After treatment according to the invention the sulfur content of the hydrocarbon stream is desirably no more than about 100 ppm, and more desirably under about 50 ppm.

In another embodiment of the invention, the hydrocarbon stream, containing the organo-sulfur compounds may first be treated to reduce its sulfur content using an alternative technology, as shown in FIG. 2, before employing the oxidative desulfurization of the present invention. The stream may be treated to reduce its sulfur content preferably to less than about 1,000 ppm, more preferably to less than about 500 ppm, and most preferably to less than about 200 ppm before subjecting the hydrocarbon to the oxidative desulfurization of the present invention. It may be advantageous for the refiner to upgrade the sulfur-containing petroleum feedstocks before treatment using the present invention by first removing as much as possible of the easy-to-remove sulfur using conventional processes such as HDS.

In accordance with this embodiment of the present invention, and with reference to FIG. 2, a sulfur-containing hydrocarbon gas stream 10 containing organo-sulfur compounds is first treated using an alternative sulfur removal system, such as conventional HDS, in treatment zone 100. As recognized by those skilled in the art, when using HDS the sulfur-containing petroleum feedstock is treated with a stream of hydrogen (stream 20) to convert the easy-to-remove sulfur compounds to hydrogen sulfide (stream 30). Suitable processes for desulfurizing hydrocarbons, particularly gasoline feedstocks, include technologies described in the following U.S. Pat Nos. 5,340,466; 5,346,609; 5,409,596; 5,411,658; 5,482,617; 5,500,108; 5,510,016; 5,510,568; 5,525,210; 5,595,634; 5,597,476; 5,770,46; 5,807,477; 5,906,730; 6,042,719; 6,103,105; 6,120,679; 6,153,089 and 6,162,352. Still other techniques will be apparent to those skilled in the art of sulfur removal. The easy-to-remove sulfur compounds include aliphatic mercaptans, naphthenic mercaptans, and aromatic mercaptans, sulfides, di-sulfides and polysulfides

The petroleum feedstock discharged from treatment zone 100, having a reduced sulfur content, but retaining most, if not all, of the refractory sulfur compounds such as thiophene, benzothiophene, dibenzothiophene and their higher boiling derivatives, in stream 40 is then preferably introduced into a concentration zone 200 for increasing the concentration of such refractory sulfur compounds. For example, in a preferred approach the refractory sulfur compounds would be concentrated from the major portion of the petroleum feedstock, possibly via complexation with ammonium complexes or by use of another known extraction or absorption technology, and distilled, or otherwise separated into a sulfur-concentrated hydrocarbon stream 60 and a sulfur-depleted petroleum feedstock 50.

The sulfur concentrated hydrocarbon stream 60 then is introduced into a reactor 600 for oxidative desulfurization. Air or an oxygen-enriched gas generally is added to the reactor via stream 70 to establish oxidizing conditions in reactor 600. Reactor 600 contains a supported metal oxide catalyst, or a bulk metal oxide catalyst, in a form suitable for conducting the oxidation reactions. The selective oxidation that occurs in reactor 600 produces a gas stream containing the oxygenated products, sulfur dioxide, H₂O, CO_(x) and unreacted hydrocarbons and sulfur compounds, which exits reactor 600 in gas stream 80. The oxygenated products may include maleic anhydride, phenol, benzyl aldehyde, benzoic acid and the like depending upon the nature of the sulfur compounds in gas stream 60 and sulfur-deficient hydrocarbons may also be produced.

As noted, the oxidizing agent used in the selective oxidation can usually be oxygen or air. The contacting of the sulfur-containing hydrocarbon gas stream with the supported metal oxide catalyst or bulk metal oxide catalyst under an oxidizing atmosphere, e.g., in the presence of oxygen, and at an appropriate temperature, causes a selective oxidation of the sulfur compounds to the valuable oxygenated products.

The optimum reaction time in reaction zone 600 (space velocity) varies with temperature, pressure and the molar ratio of the reactants. The space velocity likely will be maintained below about 4800 V/V/hr. As a general rule, higher conversions are associated with lower space velocities, e.g., a space velocity of 5 to 200 volume of gas (STP) per volume of catalyst per hour. In the broad practice of the invention, space velocities of up to 2000 volumes of gas (STP) per volume of catalyst per hour are generally contemplated.

A variety of oxygenated species, such as maleic anhydride, phenol, benzyl aldehyde and benzoic acid, are the intended products of the present process and can be recovered from the gaseous reaction product stream 80, separate from byproduct SO₂ and the CO_(x) and from unreacted hydrocarbons, sulfur-deficient hydrocarbons and unconverted sulfur-containing compounds (stream 110), using any one of a number of separation options known to those skilled in the art.

As will be recognized by those skilled in the art, the gas stream 80 leaving the reactor will contain the hydrocarbon feedstock and may contain unreacted sulfur compounds, sulfur-deficient hydrocarbons as well as the oxygenated products, sulfur dioxide, carbon oxides and water. Principal by-products of the oxidative desulfurization that may be formed are carbon monoxide, which may be accompanied by carbon dioxide (often in a minor amount) and sulfur dioxide.

The reaction mixture leaving the reactor 600 in gas stream 80 is generally subject to further processing in zone 500 in a conventional manner. For example, a concentrated stream of the oxygenated products 90 can be recovered in a washer, or by indirect cooling, or also by fractional cooling. For example, the washing can be performed with an aqueous stream, in which case a multi-stage washer can be used. An aqueous stream 90 containing the oxygenated products can be obtained in this manner separate from the sulfur dioxide and carbon oxides in stream 112. An advantage of the vapor-phase route is the ease with which SO₂ and CO_(x) can be separated from the reaction products because of their very high vapor pressure and any residual SO₂ can be readily removed with an ion exchange column. With judicious selection of metal oxide catalyst, the sulfur-containing compounds that are typically present in petroleum feed stocks are expected to be selectively oxidized to valuable chemical intermediates and sulfur-deficient hydrocarbons.

The sulfur dioxide can be disposed of by any technique known in the art. For example, the sulfur oxide (from stream 112) can be oxidized and converted to sulfuric acid. The sulfuric acid can then be used directly in the petroleum refinery for purposes well known to those skilled in the art. The crude stream of the oxygenated products then can be treated, such as by distillation, for recovering a purified stream of, for example, maleic anhydride. Fractional condensation also can be used to obtain a desired oxygenated product. Other ways for isolating the oxygenated products will be apparent to those skilled in this art. The residual gas 112, likely containing carbon monoxide as well may be treated (so as to recover sulfur oxides). The remaining fraction in stream 110 containing the hydrocarbon fraction and any unreacted sulfur compounds and sulfur-deficient hydrocarbons can be recycled to the oxidative desulfurization reactor 600 (not shown) following any heating that may be needed to convert the stream into a gas, or may be sufficient low in sulfur impurities to be returned to the refinery as for blending with other feedstocks for making gasoline.

For obtaining higher yields and selectivities, the conditions of the oxidative desulfurization can be varied. For example, the pressure, temperature, composition of the starting gas mixture, the amount of catalyst and/or the rate of flow can be varied. The reactor effluent remaining after separation of the oxygenated products and by-products can then be recycled (not shown) into the reactor 600.

In accordance with this invention, the refractory sulfur compounds are separated and then isolated from a petroleum feedstock by distillation, solvent extraction and/or adsorption-desorption and then they are oxidized by gas phase oxidation over a supported metal oxide catalyst. In a particularly preferred embodiment of the present invention, shown schematically in FIG. 3, a sulfur-containing hydrocarbon gas stream 10 containing organo-sulfur compounds is first treated using an alternative sulfur removal system, such as conventional HDS, in treatment zone 100. As recognized by those skilled in the art, when using HDS the, sulfur-containing petroleum feedstock is treated with a stream of hydrogen (stream 20) to convert the easy-to-remove sulfur compounds to hydrogen sulfide (stream 30). Suitable processes for desulfurizing hydrocarbons, particularly gasoline feedstocks, include technologies described in the following U.S. Pat. Nos. 5,340,466; 5,346,609; 5,409,596; 5,411,658; 5,482,617; 5,500,108; 5,510,016; 5,510,568; 5,525,210; 5,595,634; 5,597,476; 5,770,46; 5,807,477; 5,906,730; 6,042,719; 6,103,105; 6,120,679; 6,153,089 and 6,162,352. Still other techniques will be apparent to those skilled in the art of sulfur removal. The easy-to-remove sulfur compounds include aliphatic mercaptans, naphthenic mercaptans, and aromatic mercaptans, sulfides, di-sulfides and polysulfides. Alternatively, the easy-to-remove sulfur compounds may also be desulfurized by oxidative desulfurization.

The petroleum feedstock discharged from treatment zone 100, having a reduced sulfur content, but retaining most, if not all, of the refractory sulfur compounds such as thiophene, benzothiophene, dibenzothiophene and any higher boiling derivatives, in stream 40 is then preferably introduced into a concentration zone 200 for isolating the sulfur compounds from the hydrocarbon stream. For a petroleum feedstock that is already substantially free of the easy-to-remove organo-sulfur compounds, i.e., contains only refractory sulfur compounds, the stream can by-pass treatment zone 100 and be introduced directly into concentration zone 200.

For example, in a preferred approach for concentration zone 200 the refractory sulfur compounds could be isolated from the major portion of the petroleum feedstock, possibly via reversible complexation with ammonium complexes or by use of another known extraction or absorption technology, such as the extraction technique described in U.S. Pat. No. 5,753,103 (the full disclosure of which is incorporated herein by reference), the ionic liquid extraction technique described by Bösmann et al., in Chem. Commun., 2001, 2492-2495 (the full disclosure of which is incorporated herein by reference), or by a reversible olefin complexation, such as by modifying the OATS process (for Olefinic Alkylation of Thiophenic Sulphur) developed and commercialized by BP.

The OATS process facilitates the separation of the thiophenes (and other refractory sulfur compounds) by catalytically causing them to react with olefins present in a hydrocarbon stream to produce heavier compounds with boiling points above 200° C. In such modification, the sulfur-olefin complex would be broken, likely by heating the complex to isolate the organo-sulfur compounds.

In any event, following such processing in concentration zone 200, a stream containing principally the refractory sulfur compounds such as thiophene, benzothiophene, dibenzothiophene and their higher boiling derivatives, is produced within concentration zone 200 and exits that zone in stream 60.

In an alternate approach, the organo-sulfur compounds, principally including refractory sulfur compounds such as thiophene, benzothiophene, dibenzothiophene and their higher boiling derivatives, may first be treated using a mild selective oxidation, such as a liquid phase oxidation, to convert such organo-sulfur compounds to their sulfinyl (═SO) (sulfone) or sulfonyl (═SO₂) (sulfoxide) derivatives. Such mild oxidation processes are well known in the art These sulfinyl (═SO) (sulfone) or sulfonyl (═SO₂) (sulfoxide) derivatives then could be isolated, such as by extraction using dimethyl sulfoxide, or by distillation or adsorption, and then would be subjected to further processing in accordance with the present invention.

Aside from the sulfur-containing feed stream 40 and the concentrated sulfur product steam 60, other feed streams and by-product streams entering and exiting concentration zone 200 are not shown.

In yet another alternative arrangement, the OATS process could be used to treat the original hydrocarbon stream 10 and then the lower boiling sulfur fraction recovered from that processing operation (e.g., mercaptans, sulfides and the like) could be removed by fractionation and added to other refinery streams, slated to be treated only by conventional hydrotreatment. The remaining fraction would lead to stream 60 containing principally the refractory sulfur compounds such as thiophene, benzothiophene, dibenzothiophene, their higher boiling derivatives, or the sulfinyl (═SO) (sulfone) or sulfonyl (═SO₂) (sulfoxide) derivatives thereof

The refractory sulfur compounds, or the sulfinyl (═SO) (sulfone) or sulfonyl (═SO₂) (sulfoxide) derivatives thereof, in stream 60 are then introduced into a distillation zone 500 within which the various fractions of the stream are separated using standard rectification techniques. For illustrative purposes only, stream 60 is shown being separated into three fractions 65 a, 65 b and 65 c, respectively containing primarily thiophene, benzothiophene and higher boiling compounds and derivatives, or their corresponding sulfinyl (═SO) (sulfone) or sulfonyl (═SO₂) (sulfoxide) derivatives. Each purified steam then is introduced respectively into a reactor 600 a through 600 c for oxidative desulfurization in accordance with the present invention. Air or an oxygen-enriched gas generally is added to each of the reactors via streams 70 a through 70 c respectively to establish oxidizing conditions in each respective reactor 600 a through 600 c. Each reactor preferably contains a supported metal oxide catalyst (monolayer catalyst), or alternatively a bulk metal oxide catalyst, in a form suitable for conducting the oxidation reactions. Each reactor can be similar to those described above.

The selective oxidation that occurs in each reactor produces a gas stream containing the oxygenated product generated by oxidation of each of the respective sulfur compounds, sulfur dioxide, H₂O, and CO_(x), which exits each reactor 600 a through 600 c in gas streams 80 a, 80 b and 80 c respectively. The oxygenated products may include maleic anhydride in stream 80 a, phenol in stream 80 b, benzyl aldehyde and benzoic acid in stream 80 c and the like, depending upon the nature of the sulfur compounds in each of the gas streams 60 a through 60 c.

As noted, the oxidizing agent used in the selective oxidation can usually be oxygen or air. The contacting of the organo-sulfur compounds, in the gaseous phase, with the supported metal oxide catalyst or bulk metal oxide catalyst under an oxidizing atmosphere, e.g., in the presence of oxygen, and at an appropriate temperature, causes a selective oxidation of the sulfur compounds to the valuable oxygenated products.

Each oxidized product stream 80 a through 80 c then is treated in a separation zone 700 a through 700 c to remove sulfur dioxide and other light boiling fractions from the desired oxygenated products in stream 90 a through 90 c respectively.

The only significant emission from the process of the present invention would be undesirable greenhouse gas CO₂ due to minor unselective oxidation reaction pathways, as the sulfur dioxide can be recovered and used in the refinery as described above. Furthermore, the oxidative desulfurization of the present invention removes the need for additional hydrogen production from the costly and energy intensive methane reforming reaction, which would be required to support the planned expansion of the current hydrodesulfurization (HDS) technology to obtain the higher level of sulfur removal required by the more stringent regulatory limits.

The vapor-phase organo-sulfur oxidation route of the present invention is generally preferred relative to the known liquid oxidation approaches given the potential for large-scale production of the previously described oxygenated compounds, which are useful chemical intermediates. In addition, vapor-phase routes also avoid problems with solvents and catalyst recovery usually encountered with liquid-phase oxidation processes and the mild temperatures employed in liquid-phase oxidation, which tend to yield only sulfoxides and sulfones.

The advantages offered by this oxidative desulfurization process are: (1) the use of free O₂, rather than expensive H₂ to drive the desulfurization, (2) the elimination of, or diminution of the need for costly reactor units for methane steam reforming and water-gas shift for added hydrogen generation and for additional Claus reactions, (3) the production of significantly lower amounts of global warming CO₂ due to the minor unselective oxidation reaction pathways, (4) the direct production of H₂SO₄ that can be used in the alkylation processes in the petroleum refinery and (5) the production of a supply of relatively inexpensive sulfur-containing feedstocks for the production of valuable chemical intermediates as well as sulfur-deficient olefinic and aromatic hydrocarbons. Thus, the oxidative desulfurization process of the invention is able to remove sulfur from fuels in a way that approaches the ultimate pollution control strategy: an environmentally benign process with zero emissions.

EXAMPLES

To facilitate a more complete understanding of the invention, a number of examples showing catalyst preparation are provided below. The scope of the invention, however, is not limited to specific embodiments disclosed in these examples, which are for purposes of illustration only.

Catalyst Preparation and Characterization—Supported metal oxide catalysts can be prepared as follows:

Preparation Example 1 Vanadia on Titania

A vanadia on titania metal oxide supported catalyst can be prepared in accordance with the following procedure. A vanadia-titania catalyst can be prepared by using TiO₂ (Degussa P25) as the support. The TiO₂ support (˜10% rutile and ˜90% anatase) possesses a surface area of ˜55 m²/g. It is calcined in air at 500° C. and cooled to room temperature before impregnation with the vanadium oxide precursor. The vanadium oxide overlayer on the TiO₂ support is prepared from vanadium triisopropoxide oxide (Alfa, 95-98% purity) by the incipient wetness impregnation method. The preparation is performed under a nitrogen environment and in nonaqueous solutions, since the alkoxide precursor is air and moisture sensitive. Solutions of known amounts of vanadium triisopropoxide oxide and propanol-2, corresponding to the incipient wetness impregnation volume and the final amount of vanadium required, are prepared in a glove box filled with nitrogen. The solutions of the vanadium precursor and propanol-2 are then thoroughly mixed with the titania support and dried at room temperature in the glove box for 24 hr. The impregnated samples are heated to 300° C. in flowing nitrogen and the final calcination is performed in O₂ (Linde, 99.9% pure) at 500° C. for 15 hours. The catalyst is then pelletized, crushed and sieved to obtain catalyst particles sizes between 100 to 200 μm.

Preparation Example 1A Vanadia on Titania

Another vanadia on titania metal oxide supported catalyst can be prepared using the general procedure of Preparation Example 1 except that the final calcination is conducted at 450° C. for 2 hours.

Preparation Example 2 Molybdenum Oxide on Titania

An aqueous solution of ammonium heptamolybdate ((NH₄)₆Mo₇O₂₄.4H₂O) (Alfa) is deposited onto TiO₂ (Degussa P25) as the support (˜10% rutile and ˜90% anatase) by the incipient wetness technique. As in Example 1, the support is calcined in air at 500° C. and cooled to room temperature before impregnation with the molybdenum oxide precursor. The support possesses a surface area of ˜55 m²/g. After impregnation, the wet samples are dried at room temperature for 16 hours, further dried at 110-120° C. for 16 hours and calcined at 450° C. for 12 hours. The catalyst is then pelletized, crushed and sieved to obtain catalyst particles sizes between 100 to 200 μm.

Preparation Example 3 Chromia on Titania

An aqueous solution of chromium nitrate (Cr(NO₃)₃.9H₂O) (Allied Chemical Co.) is deposited onto TiO₂ (Degussa P25) as the support using the incipient wetness technique. As in the previous Examples, the TiO₂ support (˜10% rutile and ˜90% anatase) is calcined in air at 500° C. and cooled to room temperature before impregnation with the chromium precursor. The support possesses a surface area of ˜55 m²/g. After impregnation, the wet samples are dried at room temperature for 16 hours, further dried at 110-120° C. for 16 hours and calcined at 450° C. for 13 hours. The catalyst is then pelletized, crushed and sieved to obtain catalyst particles sizes between 100 to 200 μm.

Preparation Example 4 Rhenium Oxide on Titania

An aqueous solution of perrhenic acid (HReO₄) (Aldrich) is deposited onto TiO₂ (Degussa P25) as the support using the incipient wetness technique. As before, the TiO₂ support (˜10% rutile and ˜90% anatase) is calcined in air at 500° C. and cooled to room temperature before impregnation with the rhenium oxide precursor. The support possesses a surface area of ˜55 m²/g. After impregnation, the wet samples are dried at room temperature for 16 hours, further dried at 110-120° C. for 16 hours and calcined at 450° C. for 13 hours. The catalyst is then pelletized, crushed and sieved to obtain catalyst particles sizes between 100 to 200 μm.

Preparation Example 5 Vanadia on Zirconia

A vanadium oxide overlayer is deposited onto a zirconium oxide (ZrO₂) support (Degussa) having a surface area ˜39 m² g⁻¹ using an organic solution of vanadium triisopropoxide oxide (Alfa, 95-98% purity). In particular, the vanadium overlayer is prepared by the incipient wetness impregnation method using a solution of vanadium triisopropoxide oxide and propanol-2 in a glove box filled with nitrogen. The solutions of the vanadium precursor and propanol-2 are thoroughly mixed with the zirconia support and dried at room temperature for 16 hours, further dried at 110-120° C. for 16 hours and calcined at 450° C. for 16 hours. The catalyst is then pelletized, crushed and sieved to obtain catalyst particles sizes between 100 to 200 μm.

Preparation Example 6 Vanadia on Niobia

A vanadium oxide overlayer is deposited on a niobia (Nb₂O₅) support (55 m² g⁻¹) using vanadium triisopropoxide oxide (Alfa, 95-98% purity) and the incipient wetness technique. The niobia support is prepared by calcining niobic acid (Niobia Products Co.) at 500° C. for two hours. A solution of vanadium triisopropoxide oxide and propanol-2 is thoroughly mixed with the niobia support in a glove box filled with nitrogen, dried at room temperature for 16 hours, further dried at 110-120° C. for 16 hours and calcined at 450° C. for 16 hours. The catalyst is then pelletized, crushed and sieved to obtain catalyst particles sizes between 100 to 200 μm.

Preparation Example 7 Vanadia on Alumina

A vanadium oxide overlayer is deposited on an alumina (Al₂O₃) support (Harshaw, 180 m² g⁻¹) using an organic solution of vanadium triisopropoxide oxide (Alfa, 95-98% purity) and the incipient wetness impregnation. A solution of the vanadium precursor and propanol-2 is thoroughly mixed with the alumina support, in a glove box filled with nitrogen, dried at room temperature for 16 hours, further dried at 110-120° C. for 16 hours and calcined at 500° C. for 16 hours. The catalyst is then pelletized, crushed and sieved to obtain catalyst particles sizes between 100 to 200 μm.

Preparation Example 8 Vanadia on Silica

A vanadium oxide overlayer is deposited on a silica (SiO₂) support (Cab-O-Sil, 300 m² g⁻¹) using an organic solution of vanadium triisopropoxide oxide (Alfa, 95-98% purity) and the incipient wetness impregnation. A solution of the vanadium precursor and propanol-2 is thoroughly mixed in a glove box filled with nitrogen with the SiO₂ support, the wet silica was dried at room temperature for 16 hours, further dried at 110-120° C. for 16 hours and calcined at 500° C. for 16 hours. The catalyst is then pelletized, crushed and sieved to obtain catalyst particles sizes between 100 to 200 μm.

Preparation Example 9 Tungsten Oxide on Silica

An aqueous solution of ammonium metatungstate ((NH₄)₆H₂W₁₂O₄₀.xH₂O) (Pfaltz & Bauer, 99.9% purity) is deposited as an oxide overlayer onto a silica (SiO₂) support (Cab-O-Sil, 300 m² g⁻¹) using the incipient wetness technique. After impregnation, the silica support is dried at room temperature for 16 hours, further dried at 110-120° C. for 16 hours and calcined at 500° C. for 16 hours. The catalyst is then pelletized, crushed and sieved to obtain catalyst particles sizes between 100 to 200 μm.

Preparation Example 10 Niobia on Silica

An aqueous solution of niobium oxalate (Niobium Products Co.) is deposited onto a silica (SiO₂) support (Cab-O-Sil, 300 m² g⁻¹) using the incipient wetness technique. After impregnation, the silica support is dried at room temperature for 16 hours, further dried at 110-120° C. for 16 hours and calcined at 500° C. for 16 hours. The catalyst is then pelletized, crushed and sieved to obtain catalyst particles sizes between 100 to 200 μm.

Preparation Example 11 Titania on Silica

Titanium isopropoxide (Aldrich) in a toluene solution is impregnated onto a silica (SiO₂) support (Cab-O-Sil, 300 m² g⁻¹) under a nitrogen blanket to form a titania overlayer using the incipient wetness technique. After impregnation, the wet silica is dried at room temperature for 16 hours, further dried at 110-120° C. for 16 hours and calcined at 500° C. for 16 hours. The catalyst is then pelletized, crushed and sieved to obtain catalyst particles sizes between 100 to 200 μm.

Preparation Example 12 Vanadia and Tungsten Oxide on Titania

A vanadia and tungsten oxide on titania catalyst is prepared by a two step incipient wetness impregnation method. A vanadium oxide overlayer is deposited first on the TiO₂ support using a solution of vanadium triisopropoxide oxide (Alfa, 95-98% purity) and propanol-2 by the incipient wetness impregnation method in a glove box filled with nitrogen. The solution of the vanadium precursor and propanol-2 are thoroughly mixed with the TiO₂ (Degussa P25) as the support. The TiO₂ support (˜10% rutile and ˜90% anatase) is prepared by previous calcination in air at 500° C. and cooled to room temperature before impregnation with the vanadium oxide precursor. The support possesses a surface area of ˜55 m²/g. After impregnation, the wet TiO₂ is dried at room temperature for 16 hours, further dried at 110-120° C. for 16 hours and calcined at 450° C. for 12 hours. Subsequently, an aqueous solution of ammonium metatungstate ((NH₄)₆H₂W₁₂O₄₀.xH₂O) is deposited as an oxide overlayer onto the TiO₂ support, again using the incipient wetness technique. After impregnation, the wet samples are dried at room temperature for 16 hours, further dried at 110-120° C. for 16 hours and calcined at 500° C. for 16 hours. The catalyst is then pelletized, crushed and sieved to obtain catalyst particles sizes between 100 to 200 μm.

Preparation Example 13 Vanadia and Titania on Silica

A vanadia and titania on silica catalyst is prepared by a two step incipient wetness impregnation method. The silica support used for this study was Cabosil EH-5 (380 m²/g). This fluffy material is treated with water in order to condense its volume for easier handling. Then the wet SiO2 is dried at 120° C. and subsequently calcined at 500° C. overnight. A titanium oxide overlayer is deposited first on the silica (SiO₂) support under a nitrogen blanket using titanium isopropoxide (Aldrich) in a toluene solution by the incipient wetness impregnation method in a glove box filled with nitrogen. After impregnation, the loaded sample is dried at room temperature for 16 hours, further dried at 110-120° C. for 16 hours and calcined at 500° C. for 4 hours. Subsequently, a solution of vanadium triisopropoxide oxide (Alfa, 95-98% purity) and propanol-2 is impregnated onto the silica (SiO₂) support containing titania again using the incipient wetness technique. The solution of the vanadium precursor and propanol-2 is thoroughly mixed with the SiO₂ support containing titania. After impregnation, the wet SiO₂ is dried at room temperature for 16 hours, further dried at 110-120° C. for 16 hours and calcined at 450° C. for 2 hours. The catalyst is then pelletized, crushed and sieved to obtain catalyst particles sizes between 100 to 200 μm.

Example 1

Temperature Programmed Surface Reaction Mass Spectrometry (TPSR-MS) was carried out with an AMI-100 system (Zeton Altamira Instruments) equipped with an online mass spectrometer (Dycor DyMaxion, Ametek Process Instruments). The catalyst sample (200 mg of a 5% V₂O₅/TiO₂) was loaded in an U-type quartz tube and pretreated at 450° C. in flowing dry air for 1 h to remove moisture and ensure the catalyst was fully oxidized, and then cooled down to the adsorption temperature in He (Air gas, ultrahigh purity) flow. The temperature was probed using a thermocouple placed ˜5 mm above the top portion of the catalyst bed. The adsorption was performed at 50° C. for thiophene by flowing a certified mixture of 1000 ppm Thiophene/He (Scott Specialty Gases) for 30 minutes at a flow rate of 30 mL/min. After the reactor was purged of any excess adsorbents with He for 30 minutes the catalyst was then ramped from the adsorption temperature to 500° C. at a constant heating rate of 10° C./min in He or 5% O₂/He (Scott Specialty Gases) with a flow rate of 30 mL/min. The desorbed gases were analyzed by a quadruple mass spectrometer linked via a capillary tube from the exiting gas stream of the reactor at m/e=26 (Maleic Anhydride) and m/e=64 (SO₂), respectively. Pure gases of He and Ar were used to verify the calibration of the mass spectrometer prior to any analysis.

The results are shown in FIG. 4. The separate figures show the desorption of maleic anhydride and SO₂ after adsorption of thiophene on a 5% V₂O₅/TiO₂ catalyst at 100 C. The sample is heated at a rate of 10 C/minute in flowing oxygen/He and the reaction products are monitored by a mass spectrometer. This transient experiment proves that maleic anhydride can be formed from thiophene oxidesulfurization on supported vanadia on titania catalyst. The first plot (for maleic anhydride) shows the formation of maleic anhydride from thiophene under the stated conditions. The second plot (for SO2) shows that the sulfur contained in the thiophene ring has been removed as SO₂ during the formation of maleic anhydride mentioned earlier.

Another product from the oxidation was n-butane, a sulfur-deficient hydrocarbon, as is shown in FIG. 5.

It will be understood that while the invention has been described in conjunction with specific embodiments thereof, the foregoing description and examples are intended to illustrate, but not limit the scope of the invention. Other aspects, advantages and modifications will be apparent to those skilled in the art to which the invention pertains, and these aspects and modifications are within the scope of the invention, which is limited only by the appended claims. 

1. A process for desulfurizing a hydrocarbon stream containing heterocyclic sulfur compounds, which process comprises contacting a gaseous hydrocarbon feed stream containing said heterocyclic sulfur compounds, or sulfinyl (═SO) or sulfonyl (═SO₂) derivatives thereof, in the gas phase and in the presence of oxygen with a supported metal oxide catalyst, or with a bulk metal oxide catalyst.
 2. The process of claim 1 wherein the contacting converts at least a portion of the heterocyclic sulfur compounds, or the sulfinyl (═SO) or sulfonyl (═SO₂) derivatives thereof, to oxygenated products.
 3. The process of claim 1 wherein the contacting converts at least a portion of the heterocyclic sulfur compounds, or the sulfinyl (═SO) or sulfonyl (═SO₂) derivatives thereof, to oxygenated products and then recovering a hydrocarbon stream with substantially reduced sulfur separately from the oxygenated products.
 4. The process of claim 1 wherein the contacting converts at least a portion of the heterocyclic sulfur compounds, or the sulfinyl (═SO) or sulfonyl (═SO₂) derivatives thereof, to sulfur-deficient hydrocarbons.
 5. The process of claim 1 wherein the contacting converts at least a portion of the heterocyclic sulfur compounds, or the sulfinyl (═SO) or sulfonyl (═SO₂) derivatives thereof, to oxygenated products and sulfur-deficient hydrocarbons.
 6. The process of claim 1 wherein the contacting converts at least a portion of the heterocyclic sulfur compounds, or the sulfinyl (═SO) or sulfonyl (═SO₂) derivatives thereof, to oxygenated products and sulfur-deficient hydrocarbons and then recovering a hydrocarbon stream with substantially reduced sulfur separately from the oxygenated products.
 7. The process of claim 1, 2, 3, 4, 5 or 6 wherein the supported metal oxide catalyst comprises a metal oxide substrate, or support selected from the group consiting of titania, silica, zirconia, alumina, niobia, tantala, ceria, magnesia, manganates, lanthanum oxide, tin oxide and mixtures thereof, whose surface has been modified with a monolayer of an oxide of a catalytic metal selected from the group consisting of titanium (Ti), zirconium (Zr), molybdenum (Mo), rhenium (Re), vanadium (V), chromium (Cr), tungsten (W), manganese (Mn), niobium (Nb), tantalum (Ta) and mixtures thereof.
 8. The process of claim 7 wherein the catalytic metal is either vanadium alone or is a mixture containing vanadium.
 9. The process of claim 1, 2, 3, 4, 5 or 6 wherein the bulk metal oxide catalyst comprises a compound selected from the group consisting of molybdates (Mo), chromates (Cr), vanadates (V), rhenates (Re), titanates (Ti), niobates (Nb), tantalates (Ta), tungstates (W), manganates (Mn) and mixtures thereof.
 10. The process of claim 9 wherein the bulk metal oxide catalyst is selected from the group consisting of PbV₂O₆, NaVO₃, Na₃VO₄, BiVO₄AlVO₄, FeVO₄, Mg₃(VO₄)₂, Mg₂V₂O₇, CeVO₄, Zn₃(VO₄)₂, CdV₂O₇, Zn₂V₂O₇, VOPO₄, KVO₃, Pb₂V₂O₇, TlVO₄, PbMoO₄, CaMoO₄, Bi₂Mo₂O₉, Bi₃(FeO₄)(MoO₄)₃, Na₂MoO₄, MnMoO₄, Gd₂(MoO₄)₃, MgMoO₄, CuMoO₄, CoMoO₄, Fe₂(MoO₄)₃, Te₂MoO₇, NiMoO₄, Al₂(MoO₄)₃, Cr₂(MoO₄)₃, Na₂Mo₂O₇, YNbO₄, YbNbO₄, LiNbO₃, NaNbO₃, KNbO₃, AlNbO₄, K₈Nb₆O₁₉, BiNbO₄, SbNbO₄, NbOPO₄, CaNb₂O₆, K₄Nb₆O₁₇, KCa₂Nb₃O₁₀, Li₆WO₆, FeWO₄, CoWO₄, MnWO₄, NiWO₄, CuWO₄, CaWO₄, Cs₂WO₄, Na₂WO₄, B_(a)WO₄, Fe₂(WO₄)₃, Al₂(WO₄)₃, SrWO₄, K₂WO₄, Na₂W₂O₇, Li₂WO₄, CsLuW₂O₈, BiWO₄, Na₂CrO₄, Na₂Cr₂O₇, Na₂Cr₃O₁₀, Na₂Cr₄O₁₃, K₂CrO₄, K₂Cr₂O₇, K₂Cr₃O₁₀, K₂Cr₄O₁₃, Fe₂(CrO₄)₃, CaCrO₄, Cs₂CrO₄, BiCrO₄, NaReO₄, Li₆ReO₄, Mg(ReO₄)₂, Na₂TiO₄, NaTiO₃, BaTiO₄, BaTiO₃, Mn₃(VO₄)₂, MnAl₂O₄, KMnO₄, MnO, MnO₂, Mn₂O₃and Mn₃O₄. 